Process to Make Olefins from Isobutanol

ABSTRACT

A process for the conversion of an alcohol mixture to make propylene may include introducing into a reactor a stream that includes the alcohol mixture. The alcohol mixture may include 20 to 100 weight percent isobutanol. The process may include contacting the stream with a single catalyst at a temperature above 450° C. in the reactor at conditions effective to dehydrate the isobutanol, forming C 4   +  olefins, and to catalytically crack the C 4   +  olefins. The single catalyst may be an acid catalyst adapted to cause both the dehydration and the catalytic cracking. The process may include recovering from the reactor an effluent that includes ethylene, propylene, water, and various hydrocarbons. The process may include fractionating the effluent to produce an ethylene stream, a propylene stream, a fraction of hydrocarbons having 4 carbon atoms or more, and water.

FIELD OF THE INVENTION

The present invention relates to the simultaneous dehydration and cracking of isobutanol on a catalyst to produce an olefin stream comprising propylene. The limited supply and increasing cost of crude oil has prompted the search for alternative processes for producing hydrocarbon products such as propylene. i-Butanol can be obtained by fermentation of carbohydrates coming from the biomass, via the syngas route or base-catalysed Guerbet condensation. Made up of organic matter from living organisms, biomass is the world's leading renewable energy source.

BACKGROUND OF THE INVENTION

The bio-ethanol is one of the most relevant sources of bio-carbon today. This platform molecule available today at a price of its calorific value is venturing out of fuel application being used as precursor for base chemicals. While the ethylene can easily produced by dehydration from ethanol, the direct conversion of ethanol to propylene is problematic due to very low yield.

One step process provides a wide diversity in the formed products obtained in minor amounts which monetizing is not very obvious. Multistep process which includes ethanol dehydration to ethylene, offers better overall selectivity to propylene. However, the obtained ethylene has to be first dimerized to butene or oligomerized to be further reacted via metathesis or via cracking in OCP (olefin cracking process) reactor. The complexity of the multistep process increases significantly the manufacturing costs of bio-propylene.

The way to produce bio-propylene can be accomplished by employing a new concept: using isobutanol as a platform molecule. Of the described routes towards isobutanol, the Guerbet condensation, the synthesis gas conversion to alcohols and the 2-keto acid pathway from carbohydrates are routes that can use biomass as primary feedstock. The fermentation of sugar as well as a syngas conversion may result directly to formation of heavy alcohols (C3+), in particular i-butanol, which is often an abundant product (Applied Catalysis A, general, 186, p. 407, 1999 and Chemiker Zeitung, 106, p. 249, 1982).

Gasification of biomass results in synthesis gas that can be converted after purification into methanol, ethanol, propanol or directly into isobutanol. In addition, methanol and ethanol or propanol resourced from biomass can be further condensed to isobutanol. The base-catalysed Guerbet condensation of methanol with ethanol and/or propanol increases the concentration of i-butanol in the alcohol fraction and in particular in C3+ heavy alcohols fraction (J. of Molecular Catalysis A: Chemical 200, 137, 2003 and Applied Biochemistry and Biotechnology, 113-116, p. 913, 2004).

Isobutanol (2-methyl-1-propanol) has historically found limited applications and its use resembles that of 1-butanol. It has been used as solvent, diluent, wetting agent, cleaner additive and as additive for inks and polymers. Recently, isobutanol has gained interest as fuel or fuel component as it exhibits a high octane number (Blend Octane R+M/2 is 102-103) and a low vapor pressure (RVP is 3.8-5.2 psi).

Isobutanol is often considered as a byproduct of the industrial production of 1-butanol (Ullmann's encyclopedia of industrial chemistry, 6^(th) edition, 2002). It is produced from propylene via hydroformylation in the oxo-process (Rh-based catalyst) or via carbonylation in the Reppe-process (Co-based catalyst). Hydroformylation or carbonylation makes n-butanal and iso-butanal in ratios going from 92/8 to 75/25. To obtain isobutanol, the iso-butanal is hydrogenated over a metal catalyst.

Recently, new biochemical routes have been developed to produce selectively isobutanol from carbohydrates. The new strategy uses the highly active amino acid biosynthetic pathway of microorganisms and diverts its 2-keto acid intermediates for alcohol synthesis. 2-Keto acids are intermediates in amino acid biosynthesis pathways. These metabolites can be converted to aldehydes by 2-keto-acid decarboxylases (KDCs) and then to alcohols by alcohol dehydrogenases (ADHs). Two non-native steps are required to produce alcohols by shunting intermediates from amino acid biosynthesis pathways to alcohol production (Nature, 451, p. 86, 2008 and US patent 2008/0261230). Recombinant microorganisms are required to enhance the flux of carbon towards the synthesis of 2-keto-acids. In the valine biosynthesis 2-ketoisovalerate is an intermediate. Glycolyse of carbohydrates results in pyruvate that is converted into acetolactate by acetolactate synthase. 2,4-dihydroxyisovalerate is formed out of acetolactate, catalysed by isomeroreductase. A dehydratase converts the 2,4-dihydroxyisovalerate into 2-keto-isovalerate. In the next step, a keto acid decarboxylase makes isobutyraldehyde from 2-keto-isovalerate. The last step is the hydrogenation of isobutyraldehyde by a dehydrogenase into isobutanol.

The direct 2-keto acid pathway can produce isobutanol from carbohydrates that are isolated from biomass. Simple carbohydrates can be obtained from plants like sugar cane, sugar beet. More complex carbohydrates can be obtained from plants like maize, wheat and other grain bearing plants. Even more complex carbohydrates can be isolated from substantially any biomass, through unlocking of cellulose and hemicellulose from lignocelluloses.

The isobutanol can be dehydrated to corresponding mixture of olefins containing the same number of atoms. Dehydration of butanols has been described on alumina-type catalysts (Applied Catalysis A, General, 214, p. 251-257, 2001). Both double-bond shift and skeletal isomerisation has been obtained at very low space velocity (or very long reaction time) corresponding to a GHSV (Gas Hourly Space Velocity=ratio of feed rate (gram/h) to weight of catalyst (ml)) of less than 1 gram·ml⁻¹·h⁻¹. The dehydration reactions of alcohols to produce alkenes with the same number of carbons have been known for a long time (J. Catal. 7, p. 163, 1967 and J. Am. Chem. Soc. 83, p. 2847, 1961). Many available solid acid catalysts can be used for alcohol dehydration (Stud. Surf. Sci. Catal. 51, p. 260, 1989), the European patent EP0150832, Bulletin of the Chemical Society of Japan, vol 47(2), 424-429 (1974). However, γ-aluminas are the most commonly used, especially for the longer chain alcohols (with three and more carbon atoms). This is because catalysts with stronger acidity, such as the silica-aluminas, molecular sieves, zeolites or resin catalysts can promote double-bond shift, skeletal isomerization and other olefin interconversion reactions.

The primary product of the acid-catalysed dehydration of isobutanol is iso-butene and water:

So, the dehydration may result in substantially pure isobutene stream or in blended olefinic stream reach in butenes if a secondary reaction occurs on the catalyst.

The production of light olefins (ethylene and propylene) from a mixed alcohol feedstock in an oxygenates to olefins process has been described in the U.S. Pat. No. 7,288,689. Said patent provides various processes for producing C1 to C4 alcohols, optionally in a mixed alcohol stream, and optionally converting the alcohols to light olefins. In one embodiment, it includes directing a first portion of a syngas stream to a methanol synthesis zone wherein methanol is synthesized. A second portion of the syngas stream is directed to a fuel alcohol synthesis zone wherein fuel alcohol is synthesized. The methanol and at least a portion of the fuel alcohol are directed to an oxygenate to olefin reaction system for conversion thereof to ethylene and propylene. In this prior art “fuel alcohol” means an alcohol-containing composition comprising ethanol, one or more C3 alcohols, one or more C4 alcohols and optionally one or more C5+ alcohols. At col 21 lines 14+ is mentioned “ . . . Additionally or alternatively, the fuel alcohol-containing stream comprises one or more C4 alcohols, preferably on the order of from about 0.1 to about 20 weight percent C4 alcohols, preferably from about I to about 10 weight percent C4 alcohols, and most preferably from about 2 to about 5 weight percent C4 alcohols, based on the total weight of the fuel alcohol-containing stream. The fuel alcohol-containing stream preferably comprises at least about 5 weight percent C3-C4 alcohols, more preferably at least about 10 weight percent C3-C4 alcohols, and most preferably at least about 15 weight percent C3-C4 alcohols . . . ”. Preferably, the molecular sieve catalyst composition comprises a small pore zeolite or a molecular sieve selected from the group consisting of: MeAPSO, SAPO-5, SAPO-8, SAPO-11, SAPO-16, SAPO-17, SAPO-18, SAPO-20, SAPO-031, SAPO-34, SAPO-35, SAPO-36, SAPO-37, SAPO-40, SAPO-41, SAPO-42, SAPO-44, SAPO-47, SAPO-56, AEI/CHA intergrowths, metal containing forms thereof, intergrown forms thereof, and mixtures thereof.

EP 2070896 A1 describes the dehydration of 1-butanol on a porous crystalline aluminosilicate (TON type) in the hydrogen form. At 500° C. the products are in wt %:

propylene 10.76 trans-butene-2 16.99 butene-1 13.49 isobutene 31.30 cis-butene-2 13.33

U.S. Pat. No. 6,768,037 describes a process for upgrading a Fischer-Tropsch product comprising paraffins, oxygenates (alcohols), and C6+ olefins. The process includes contacting the Fischer-Tropsch product with an acidic olefin cracking catalyst (ZSM-5) to convert the oxygenates and C6+ olefins to form light olefins. The contacting conditions include a temperature in the range of about 500° F. to 850° F., a pressure below 1000 psig, and a liquid hourly space velocity in the range of from about 1 to 20 hr⁻¹. The process further includes recovering the Fischer-Tropsch product comprising unreacted paraffins, and recovering the light olefins. At col 6 lines 16+ is mentioned “ . . . The product from a Fischer-Tropsch process contains predominantly paraffins; however, it may also contain C₆₊ olefins, oxygenates, and heteroatom impurities. The most abundant oxygenates in Fischer-Tropsch products are alcohols, and mostly primary linear alcohols. Less abundant types of oxygenates in Fischer-Tropsch products include other alcohol types such as secondary alcohols, acids, esters, aldehydes, and ketones . . . ”.

U.S. Pat. No. 4,698,452 relates to a novel process for the conversion of ethanol or its mixtures with light alcohols and optionally water into hydrocarbons with specific and unusual selectivity towards ethylene. More particularly, it relates to the use of ZSM-5 zeolite based catalysts into which Zn alone or Zn and Mn are incorporated. The preferred reaction conditions used in the experiments are as follows: temperature=300° C.-450° C. (most preferred 400° C.); catalyst weight=4 g; total pressure=1 atm; alcohol or aqueous ethanol pressure=0.9 atm; inert gas (stripping gas)=nitrogen; weight hourly space velocity (W.H.S.V.)=2.4 h-1; duration of a run=4 hours. At table 3 dehydration of isobutanol has been made on ZSM-5 (Zn—Mn) and produces paraffins C1-C4, ethylene, propylene, butenes, aromatics and aliphatics.

It has now been discovered that isobutanol or a mixture of isobutanol and other alcohols containing two and more carbon atoms can be simultaneously dehydrated and cracked to propylene in a one-pot reactor to produce propylene rich feedstock over hydrothermally stable catalyst.

BRIEF SUMMARY OF THE INVENTION

The present invention relates to a process for the conversion of an alcohol mixture (A) comprising about 20 w % to 100% isobutanol to make essentially propylene, comprising:

a) introducing in a reactor (A) a stream comprising the mixture (A), optionally water, optionally an inert component, b) contacting said stream with a catalyst (A1) at a temperature above 450° C. in said reactor (A) at conditions effective to dehydrate at least a part of the isobutanol and other alcohols, if any, and make a cracking, c) recovering from said reactor (A) an effluent comprising: ethylene, propylene, water, optionally unconverted alcohols of the mixture (A), various hydrocarbons, and the optional inert component of step a), d) fractionating said effluent of step c) to produce at least an ethylene stream, a propylene stream, a fraction consisting essentially of hydrocarbons having 4 carbon atoms or more, water and the optional inert component of step a), optionally recycling ethylene in whole or in part at the inlet of the reactor (A), optionally recycling the fraction consisting essentially of hydrocarbons having 4 carbon atoms or more at the inlet of the reactor (A).

Advantageously, before recycling said hydrocarbons having 4 carbon atoms or more at the inlet of the reactor (A), said hydrocarbons having 4 carbon atoms or more are sent to a second fractionator to purge the heavies, water and optionally oxygenates.

In an embodiment the alcohol feed is subjected to purification to reduce the content in the metal ions, in more particularly in Na, Fe, K, Ca and Al.

In a specific embodiment the alcohol mixture (A) comprises 40 to 100 w % of isobutanol.

In a specific embodiment the alcohol mixture (A) comprises 60 to 100 w % of isobutanol.

In a specific embodiment the alcohol mixture (A) comprises 80 to 100 w % of isobutanol.

In a specific embodiment the alcohol mixture (A) comprises essentially isobutanol.

Optionally, the alcohol mixture (A) can be fed to the catalyst in presence of steam (at least 10 wt % of i-Butanol).

i-Butanol may have fossil origin, but in preferred embodiment at least a part of used feedstock is derived from biomass.

Advantageously, the alcohols of the mixture (A) are derived from the biomass and thus it gives the opportunities to introduce a part of renewable carbon in the light olefin product.

Advantageously isobutanol is obtained by fermentation of carbohydrates coming from the biomass, or from the syngas route or from the base-catalysed Guerbet condensation.

In an embodiment isobutanol is produced by the direct 2-keto acid pathway from carbohydrates that are isolated from biomass.

One skilled in the art will also appreciate that the olefin products made by the present invention can be polymerized, optionally with comonomers, to form polyolefins, particularly polyethylenes and polypropylenes.

DETAILED DESCRIPTION OF THE INVENTION

As regards the stream introduced at step a), and the alcohols in the mixture (A) besides isobutanol, one can cite ethanol, propanol, isopropanol, 1-butanol and 2-butanol and the higher alcohols.

the inert component is any component provided there is no adverse effect on the catalyst. Because the dehydration is endothermic the inert component can be used to bring energy. By way of examples the inert component is selected among the saturated hydrocarbons having up to 10 carbon atoms, naphtenes, nitrogen and CO₂. An example of inert component can be any individual saturated compound, a synthetic mixture of the individual saturated compounds as well as some equilibrated refinery streams like straight naphtha, butanes etc. Advantageously it is a saturated hydrocarbon or a mixture of saturated hydrocarbons having from 3 to 7 carbon atoms, more advantageously having from 4 to 6 carbon atoms and is preferably pentane.

The weight proportions of respectively alcohols, water and inert component are, for example, 5-100/0-95/0-95 (the total being 100). The stream comprising the alcohol mixture (A) can be liquid or gaseous.

The isobutanol-containing feed can be produced by the Guerbet condensation, the synthesis gas route and the biochemical routes. The feedstock before feeding to cracking reactor can be subjected to a different upgrading procedure including but non-limiting to purification from the metals, separation/extractions of the individual compounds, alcohols interconversion, partial dehydration to ethers, drying etc. The feedstock is essentially free of light alcohols and hydrocarbons. The weight content of these compounds in the mixture is below 10 wt %.

As regards the reactor (A), it can be a fixed bed reactor, a moving bed reactor or a fluidized bed reactor. A typical fluid bed reactor is one of the FCC type used for fluidized-bed catalytic cracking in the oil refinery. A typical moving bed reactor is of the continuous catalytic reforming type. The dehydration/cracking may be performed continuously in a fixed bed reactor configuration using a pair of parallel “swing” reactors. The various preferred catalysts of the present invention have been found to exhibit high stability. This enables the dehydration/cracking process to be performed continuously in two parallel “swing” reactors wherein when one reactor is operating, the other reactor is undergoing catalyst regeneration. The catalyst of the present invention also can be regenerated several times.

As regards the catalyst (A1) of step b), it can be any acid catalyst capable to cause the simultaneous dehydration and cracking of alcohols under above said conditions. By way of example it can be; zeolites, P-zeolites, Me-zeolites, alumina, silica-alumina, clays.

The catalyst is employed under particular reaction conditions whereby, further to the dehydration of isobutanol, the catalytic cracking of the C₄ ⁺ olefins readily proceeds. Different reaction pathways can occur on the catalyst. Olefinic catalytic cracking may be understood to comprise a process yielding shorter molecules via bond breakage.

The process conditions are selected in order to provide high selectivity towards propylene or ethylene, as desired, a stable olefin conversion over time, and a stable olefinic product distribution in the effluent. Such objectives are favoured with a low pressure, a high inlet temperature and a short contact time, all of which process parameters are interrelated and provide an overall cumulative effect. The process conditions are selected to disfavour hydrogen transfer reactions leading to the formation of paraffin's, aromatics and coke precursors.

According to an embodiment the catalyst (A1) is a crystalline Porous Aluminophosphate containing advantageously at least one 10 and/or 12 members ring into the structure.

The porous crystalline aluminophosphate may be one that is comprised of aluminum and phosphorus that are partly substituted by silicon, boron, Ni, Zn, Mg, Mn such as a porous crystalline metalaluminophosphate. The structure of such crystalline porous aluminophosphates may, for example, be those that are identified by codes for zeolites described above as AEL, AFI, AFO or FAU.

The above porous crystalline aluminophosphate is preferably a porous crystalline silicoaluminophosphate. Specifically, SAPO5, and the like having an AFI structure, SAPO41, and the like having an AFO structure, SAPO11, and the like having an AEL structure, structure or SAPO37, and the like having a FAU structure may be mentioned.

In an embodiment, the small pore molecular sieves can be selected from the group of CHA (SAPO 34, 44), AEI (SAPO 18), LEV (SAPO 35), ERI (SAPO 17) or a mixture of thereof including intergrowth phases.

According to another specific embodiment, suitable catalysts for the present process is the silicoaluminophosphate molecular sieves, in particular of the AEL group with typical example the SAPO-11 molecular sieve. The SAPO-11 molecular sieve is based on the ALPO-11, having essentially an Al/P ratio of 1 atom/atom. During the synthesis silicon precursor is added and insertion of silicon in the ALPO framework results in an acid site at the surface of the micropores of the 10-membered ring sieve. The silicon content ranges from 0.1 to 10 atom % (Al+P+Si is 100).

Various commercial zeolite products nay be used, or it is possible to use zeolites that have been synthesized by a known method disclosed in e.g. “Verified Synthesis of Zeolitic Materials” (2^(nd) Revised Edition 2001 Elsevier) published by the above IZA.

According to an embodiment the catalyst (A1) is a crystalline silicate containing advantageously at least one 10 members ring into the structure. It is by way of example of the MFI (ZSM-5, silicalite-1, boralite C, TS-1), MEL (ZSM-11, silicalite-2, boralite D, TS-2, SSZ-46), FER (Ferrierite, FU-9, ZSM-35), MTT (ZSM-23), MWW (MCM-22, PSH-3, ITQ-1, MCM-49), TON (ZSM-22, Theta-1, NU 10), EUO (ZSM-50, EU-1), MFS (ZSM-57), CON (CIT-1) and ZSM-48 family of microporous materials consisting of silicon, aluminium, oxygen and optionally boron. Advantageously in said first embodiment the catalyst (A1) is a crystalline silicate, metal containing crystalline silicate or a dealuminated crystalline silicate.

The crystalline silicate can have a ratio Si/Al of at least about 100 and is advantageously selected among the MFI and the MEL and modified with the metals Mg, Ca, La, Ni, Ce, Zn, Co, Ag, Fe, Cu. The metal content is at least 0.1 wt %.

The dealuminated crystalline silicate is advantageously such as about 10% by weight of the aluminium is removed. Such dealumination is advantageously made by a steaming optionally followed by a leaching.

In another specific embodiment the crystalline silicate catalyst is mixed with a binder, preferably an inorganic binder, and shaped to a desired shape, e.g. pellets. The binder is selected so as to be resistant to the temperature and other conditions employed in the dehydration/cracking process of the invention. The binder is an inorganic material selected from clays, silica, metal silicate, metal borates, metal oxides such as Zr0₂ and/or metals, or gels including mixtures of silica and metal oxides.

According to an embodiment the catalyst (A1) is a P-modified zeolite (Phosphorus-modified zeolite). Said phosphorus modified molecular sieves can be prepared based on MFI, MOR, MEL, clinoptilolite or FER, MWW, TON, EUO, MFS and ZSM-48 family of microporous molecular sieves having an initial Si/Al ratio advantageously between 4 and 500. The P-modified zeolites of this recipe can be obtained based on cheap crystalline silicates with low Si/Al ratio (below 30).

By way of example said P-modified zeolite is made by a process comprising in that order:

-   -   selecting a zeolite (advantageously with Si/Al ratio between 4         and 500) among H⁺ or NH₄ ⁺-form of MFI, MEL, FER, MOR,         clinoptilolite, MWW, TON, EUO, MFS and ZSM-48;     -   introducing P at conditions effective to introduce         advantageously at least 0.05 wt % of P;     -   separation of the solid from the liquid if any;     -   an optional washing step or an optional drying step or an         optional drying step followed by a washing step;     -   a calcination step.

The zeolite with low Si/Al ratio has been made previously with or without direct addition of an organic template.

Optionally the process to make said P-modified zeolite comprises the steps of steaming and leaching. The method consists in steaming followed by leaching. It is generally known by the persons in the art that steam treatment of zeolites, results in aluminium that leaves the zeolite framework and resides as aluminiumoxides in and outside the pores of the zeolite. This transformation is known as dealumination of zeolites and this term will be used throughout the text. The treatment of the steamed zeolite with an acid solution results in dissolution of the extra-framework aluminiumoxides. This transformation is known as leaching and this term will be used throughout the text. Then the zeolite is separated, advantageously by filtration, and optionally washed. A drying step can be envisaged between filtering and washing steps. The solution after the washing can be either separated, by way of example, by filtering from the solid or evaporated.

P can be introduced by any means or, by way of example, according to the recipe described in U.S. Pat. No. 3,911,041, U.S. Pat. No. 5,573,990 and U.S. Pat. No. 6,797,851.

The catalyst made of a P-modified zeolite can be the P-modified zeolite itself or it can be the P-modified zeolite formulated into a catalyst by combining with other materials that provide additional hardness or catalytic activity to the finished catalyst product. Advantageously, at least a part of phosphorous is introduced into zeolite before shaping. In a specific embodiment, the formed P-precursor can be further modified with the metals selected from Mg, Ca, La, Ni, Ce, Zn, Co, Ag, Fe, Cu according to the recipe described in WO 09092779 and WO 09092781.

The separation of the liquid from the solid is advantageously made by filtering at a temperature between 0-90° C., centrifugation at a temperature between 0-90° C., evaporation or equivalent.

Optionally, the zeolite can be dried after separation before washing. Advantageously said drying is made at a temperature between 40-600° C., advantageously for 1-10 h. This drying can be processed either in a static condition or in a gas flow. Air, nitrogen or any inert gases can be used.

The washing step can be performed either during the filtering (separation step) with a portion of cold (<40° C.) or hot water (>40 but <90° C.) or the solid can be subjected to a water solution (1 kg of solid/4 liters water solution) and treated under reflux conditions for 0.5-10 h followed by evaporation or filtering. Final equilibration step is performed advantageously at the temperature 400-800° C. either in a static condition or in a gas flow. Air, nitrogen or any inert gases can be used.

According to a Specific Embodiment the Phosphorous Modified Zeolite is Made by a Process Comprising in that Order

-   -   selecting a zeolite (advantageously with Si/Al ratio between 4         and 500, from 4 to 30 in a specific embodiment) among H⁺ or NH₄         ⁺-form of MFI, MEL, FER, MOR, clinoptilolite, MWW, TON, EUO, MFS         and ZSM-48;     -   steaming at a temperature ranging from 400 to 870° C. for         0.01-200 h;     -   leaching with an aqueous acid solution at conditions effective         to remove a substantial part of Al from the zeolite;     -   introducing P with an aqueous solution containing the source of         P at conditions effective to introduce advantageously at least         0.05 wt % of P;     -   separation of the solid from the liquid;     -   an optional washing step or an optional drying step or an         optional drying step followed by a washing step;     -   a calcination step.

Optionally between the steaming step and the leaching step there is an intermediate step such as, by way of example, contact with silica powder and drying.

Optionally the leaching and introducing P are made simultaneously by using an acid based comprising phosphorus to make the leaching.

Advantageously the selected MFI, MEL, FER, MOR, clinoptilolite, MWW, TON, EUO, MFS and ZSM-48 (or H⁺ or NH₄ ⁺-form MFI, MEL, FER, MOR, clinoptilolite, MWW, TON, EUO, MFS and ZSM-48) has an initial atomic ratio Si/Al of 100 or lower and from 4 to 30 in a specific embodiment. The conversion to the H⁺ or NH₄ ⁺-form is known per se and is described in U.S. Pat. No. 3,911,041 and U.S. Pat. No. 5,573,990.

Advantageously the final P-content is at least 0.05 wt % and preferably between 0.3 and 7 w %. Advantageously at least 10% of Al, in respect to parent zeolite MFI, MEL, FER, MOR and clinoptilolite, MWW, TON, EUO, MFS and ZSM-48, have been extracted and removed from the zeolite by the leaching.

Then the zeolite either is separated from the washing solution or is dried without separation from the washing solution. Said separation is advantageously made by filtration. Then the zeolite is calcined, by way of example, at 400° C. for 2-10 hours.

In the steam treatment step, the temperature is preferably from 420 to 870° C., more preferably from 480 to 760° C. The pressure is preferably atmospheric pressure and the water partial pressure may range from 13 to 100 kPa. The steam atmosphere preferably contains from 5 to 100 vol % steam with from 0 to 95 vol % of an inert gas, preferably nitrogen. The steam treatment is preferably carried out for a period of from 0.01 to 200 hours, advantageously from 0.05 to 200 hours, more preferably from 0.05 to 50 hours. The steam treatment tends to reduce the amount of tetrahedral aluminium in the crystalline silicate framework by forming alumina.

The leaching can be made with an organic acid such as citric acid, formic acid, oxalic acid, tartaric acid, malonic acid, succinic acid, glutaric acid, adipic acid, maleic acid, phthalic acid, isophthalic acid, fumaric acid, nitrilotriacetic acid, hydroxyethylenediaminetriacetic acid, ethylenediaminetetracetic acid, trichloroacetic acid trifluoroacetic acid or a salt of such an acid (e.g. the sodium salt) or a mixture of two or more of such acids or salts. The other inorganic acids may comprise an inorganic acid such as nitric acid, hydrochloric acid, methansulfuric acid, phosphoric acid, phosphonic acid, sulfuric acid or a salt of such an acid (e.g. the sodium or ammonium salts) or a mixture of two or more of such acids or salts.

The residual P-content is adjusted by P-concentration in the aqueous acid solution containing the source of P, drying conditions and a washing procedure if any. A drying step can be envisaged between filtering and washing steps.

Said P-modified zeolite can be used as itself as a catalyst. In another embodiment it can be formulated into a catalyst by combining with other materials that provide additional hardness or catalytic activity to the finished catalyst product. Materials which can be blended with the P-modified zeolite can be various inert or catalytically active materials, or various binder materials. These materials include compositions such as kaolin and other clays, various forms of rare earth metals, phosphates, alumina or alumina sol, titania, zirconia, quartz, silica or silica sol, and mixtures thereof. These components are effective in densifying the catalyst and increasing the strength of the formulated catalyst. The catalyst may be formulated into pellets, spheres, extruded into other shapes, or formed into a spray-dried particles. The amount of P-modified zeolite which is contained in the final catalyst product ranges from 10 to 90 weight percent of the total catalyst, preferably 20 to 70 weight percent of the total catalyst.

The catalyst (A1) which are not P-modified zeolites can be formulated with a binder as explained above for the P-modified zeolites.

The other catalyst components of the catalyst (A1) could be binders, fillers or other catalytically active materials. Clays, modified clays, basic compounds, transition metal-containing compounds as well as small pore-zeolites and silicoaluminophosphates may be implemented as other catalytically active materials.

A catalyst has already been described in WO2009098262.

As regards the pressure in steps a) and b), the use of a low alcohol partial pressure which leads to a low olefin partial pressure, for example atmospheric pressure, tends to lower the incidence of hydrogen transfer reactions in the cracking process, which in turn reduces the potential for coke formation which tends to reduce catalyst stability. The partial pressure of the alcohols is advantageously lower than 4 bars absolute (0.4 MPa) and more advantageously from 0.5 to 4 bars absolute (0.05 MPa to 0.4 MPa), preferably lower than 3.5 bars absolute (0.35 MPa) and more preferably lower than 2 bars absolute (0.2 MPa). The pressure of the reactor of step b) can be any pressure but it is more economical to operate at moderate pressure. By way of example the pressure of the reactor ranges from 1 to 30 bars absolute (0.1 MPa to 3 MPa), advantageously from 1 to 20 bars absolute (0.1 MPa to 2 MPa).

As regards the temperature in step b), the reaction is preferably performed at an inlet temperature of the feedstock of from 450° to 650° C., more preferably from 500° to 650° C., more preferably from 520° to 600° C., yet more preferably from 540° C. to 590° C.

As regards the WHSV of alcohols in step b), it ranges advantageously from 0.1 to 50 h-1, more advantageously from 1 to 20 h-1, preferably from 5 to 20 h-1, and more preferably from 5 to 15 h-1.

In order to maximize the amount of ethylene and propylene and to minimize the production of methane, aromatics and coke, it is desired to minimize the presence of diolefins in the feed. Diolefin conversion to monoolefin hydrocarbons may be accomplished with a conventional selective hydrogenation process such as disclosed in U.S. Pat. No. 4,695,560 hereby incorporated by reference.

As regards step d), the fractionation of said effluent of step c) said fractionation is carried out by any means, they are known per se.

In an embodiment the present invention comprises a further step wherein ethylene is reacted with 2-butene from the fraction consisting essentially of hydrocarbons having 4 carbon atoms or more recovered at step d). Said reaction known as methathesis produces propylene.

As regards the preparation of the metathesis feedstock, it is preferred to remove the iso-butene before metathesis. This can be done by a selective chemical transformation of iso-butene or by distillation. Selective chemical transformations are: (i) oligomerisation, (ii) etherification or (iii) hydration or combinations of them. The resulting products are respectively: (i) iso-octenes for use in gasoline, tri, tetra or pentamers of substantially iso-butene for use in Jet fuel or kerozine; (ii) methyl-t-butylether or ethyl-t-butylether; (iii) t-butanol. The oligomers are eventually hydrogenated to the corresponding paraffin's. The t-butanol can eventually be recycled back into the reactor (A).

A preferred distillation method is the catalytic distillation during which the 1-butene is continuously transformed into 2-butenes so as to optimise the 2-butenes yield and minimise entrainment of 1-butene with the overhead iso-butene. The iso-butene rich overhead can be recycling back to the reactor (A).

As regards the metathesis catalyst, three types of metal containing catalysts can be suitable to perform the disproportionation reaction. The co-metathesis reaction of the ethylene with the butene-2 or the autometathesis of a mixture of 1-butene and 2-butene can be catalyzed by three metallic oxides that are dispersed on carriers: by molybdenum (eventually in combination with cobalt and rhenium), tungsten or rhenium oxides.

A first kind of catalyst is Rhenium supported on alumina-containing carrier. The Rhenium content can be from 0.5 to 15 wt %.

The metathesis reaction, by way of example, over rhenium heptoxide catalysts is carried out preferably in a liquid phase, in absence of oxygen-containing compounds and moisture, and at a temperature of 0 to 150° C., preferably 20 to 100° C., under a pressure at least to keep the reaction mixture at the reaction temperature in the liquid state.

A second type of catalyst is tungsten supported on silica carrier. The tungsten content can be from 1 to 15 wt %. The tungsten based catalysts are advantageously used in combination with a co-catalyst. Lithium, sodium, potassium, cesium, magnesium, calcium, strontium, barium, zinc, lanthanum and yttrium are preferred.

A third type of catalyst is molybdenum supported on alumina or silica carrier. Suitable molybdenum oxide based catalysts are disclosed in U.S. Pat. No. 3,658,927 and U.S. Pat. No. 4,568,788.

The activity of the metathesis catalyst is generally decreased by polar compounds like moisture, carbon dioxide, carbon monoxide, diene compounds, sulphur and nitrogen compounds, alcohols, aldehydes and carboxylic compounds. Accordingly, the olefins used as feedstock preferably should be purified from impurities. Such impurities are removed by distillation, adsorption, extraction or washing. Other materials used during the process like nitrogen gas and hydrogen gas that are introduced into the reactor need also extensive purification. Nitrogen is often needed to purge reactors from moisture, reducing agents (carbon monoxide, ethylene or hydrogen) and resulting residues from this reduction.

Furthermore, the activity of the metathesis catalyst can further be increased or stabilised by in the presence of hydrogen. The amount of hydrogen in the combined feedstock of olefins (butenes and ethylene) is advantageously in the range of 0.1 to 10 vol % and preferably 0.2 to 5 vol %.

The metathesis reaction can be carried out in liquid phase, gas phase, and mixed gas-liquid phase, which is determined by the reaction temperature and pressure. Rhenium based catalyst performs preferably between 0 and 150° C. at a pressure to keep the feedstock in the liquid state. Molybdenum based catalyst perform preferably at 100 to 250° C. in the gas phase at from 1 to 30 bars pressure. Tungsten based catalysts perform preferably at 150 to 400° C. at a pressure of from 5 to 35 bars. The metathesis may be performed continuously in a fixed bed reactor configuration using a pair of parallel “swing” reactors, provided the catalyst exhibits sufficient stability of at least 2 days. This enables the methathesis process to be performed continuously in two parallel “swing” reactors wherein when one reactor is operating; the other reactor is undergoing catalyst regeneration. When the catalyst stability is shorter than about 2 days, metathesis may also be performed continuously in a moving bed reactor in which the catalyst circulates from a reaction zone to a regeneration zone and backwards with a residence time of the catalyst in the reaction zone of at least 5 hours. In each zone the catalyst behaves substantially like in a fixed bed reactor, but the catalyst moves slowly, by gravity or pneumatically through the respective zone. The use of a moving bed reaction allows accomplishing a continuous operation with no switching of the feedstock and regeneration gas from one reactor to another one. The reaction zone receives continuously the feedstock while the regeneration zone receives continuously the regeneration gas.

The metathesis can be done with only a mixture of n-butenes and is commonly known as autometathesis. The products are propylene and pentenes. The propylene desired product is recovered while the pentenes can be recycled back to the metathesis reaction section. The metathesis can also been carried out by adding ethylene to the n-butenes feedstock, commonly known as co-metathesis. The molar ratio of ethylene to n-butenes is advantageously from 0.75 to 5, preferably from 1 to 2.5.

As regards the products of the metathesis reaction, the reactor effluent contains non-converted ethylene, if any was added to the reaction section, and butenes, some heavies and the desired propylene product. In a de-ethaniser the ethylene, eventually hydrogen when used, is produced overhead and recycled back to the metathesis reactor. The bottom product is further separated in a de-propaniser where the overhead product is the desired propylene. The bottom product is typically butenes and some heavier olefins. The butenes can be recycled back to the metathesis reactor for further reaction.

EXAMPLES Experimental

The stainless-steel reactor tube has an internal diameter of 10 mm. 10 ml of catalyst, as pellets of 35-45 mesh, is loaded in the tubular reactor. The void spaces before and after the catalyst are filled with SiC granulates of 2 mm. The temperature profile is monitored with the aid of a thermocouple well placed inside the reactor. The reactor temperature is increased at a rate of 60° C./h to 550° C. under air, kept 2 hours at 550° C. and then purged by nitrogen. The nitrogen is then replaced by the feed at the indicated operating conditions. The catalytic tests are performed down-flow, with a pressure of about 1.5 bara, with a temperature of about 575° C. and with a weight hour space velocity (WHSV) of about 7 h⁻¹.

Analysis of the products is performed by using an on-line gas chromatography.

Example 1

The catalyst is a phosphorous modified zeolite (P-ZSM5), prepared according to the following recipe. A sample of zeolite ZSM-5 (Si/Al=13) in H-form was steamed at 550° C. for 6 h in 100% H₂O. Then, 600 g of the steamed solid was subjected to a contact with 114 g of an aqueous solution of H₃PO₄ (85% wt) for 2 h under reflux condition (4 ml/1 g zeolite) followed by addition of 34 g of CaCO3. Then the solution was dried by evaporation under rigours stirring for 3 days at 80° C. 685 g of the dried sample was extruded with 401.5 g of silica sol Bindzil (34 wt % SiO2), and 3 wt % of extrusion additives. The shaped sample contained about 80 wt % zeolite. The extruded solid was dried at 110° C. for 16 h and steamed at 600° C. for 2 h.

For the following experiment, an isobutanol feed has been tested in mixture with water (ratio 95/5 wt %), under 1.5 bara, with a isobutanol space velocity of 7 h-1 and a temperature of about 575° C. The table 1 presents the average catalyst performance for 40 hours-on-stream. The results are given in the table 1 on CH2-basis and coke free basis. The catalyst has not presented signs of deactivation after about 90 hours in operation.

Comparative Example

The test under the same condition on the same catalyst has been done with ethanol/H2O blend. The table 1 presents the average catalyst performance for 40 hours-on-stream. The results are given in the table 1 on CH2-basis and coke free basis.

TABLE 1 Example 1 Comparative 95 wt % 95 wt % FEED i-Butanol/5 wt % H2O Ethanol/5 wt % H2O P, bara 2 2 T, ° C. 575 575 WHSV, h−1 7.4 7.4 Conversion, % 100 100 Selectivity on CH2 basis, % Ethylene 7.9 93 Propylene 33.3 2.5

The conversions are complete in both cases, but the propylene selectivity was only about 2.5% using ethanol as a feedstock and 33.3% using isobutanol. These examples illustrate that potentially bio-propylene can be produced more efficiently from bio-i-butanol than from bio-ethanol.

Example 2

The catalyst is a phosphorous modified zeolite (P-ZSM5), prepared according to the following recipe. A sample of zeolite ZSM-5 (Si/Al=13) in H-form was steamed at 550° C. for 6 h in 100% H2O. Then, 1270 g of the steamed solid was subjected to a contact with 241.3 g of an aqueous solution of H₃PO₄ (85% wt) for 2 h under reflux condition (4 ml/1 g zeolite) followed by addition of 69.9 g of CaCO3. Then the solution was dried by evaporation under rigours stirring for 3 days at 80° C. 750 g of the dried sample was extruded with 401.5 g of silica sol Bindzil (34 wt % SiO2) and 3 wt % of extrusion additives. The shaped sample contained about 80 wt % zeolite. The extruded solid was dried at 110° C. for 16 h and steamed at 600° C. for 2 h.

For the following experiments, an isobutanol feed has been tested in mixture with water (ratio 95/5 wt %), under 1.5 bara, with a isobutanol space velocity of 7 h-1 and a temperature of about 575° C.

The isobutanol conversion is complete and the major products are propylene and C4 olefins. The C3=selectivity reaches about 36 wt % (on CH2 basis) and the C4=selectivity about 27 wt % (on CH2 basis).

The table 2 presents the average catalyst performance for 40 hours-on-stream. The results are given in the table 1 on CH2-basis and coke free basis. The catalyst has not presented signs of deactivation after about 90 hours in operation.

TABLE 2 i-BuOH/H2O FEED 95/5% wt P (bara) 1.5 T (° C.) 575 WHSV (H−1) 7.4 Conversion 100 HC Selectivity on CH2-basis Ethylene 10.6 Propylene 36.3 C4 olefins 27.1 

1-19. (canceled)
 20. A process for the conversion of an alcohol mixture comprising about 20 to 100 weight percent isobutanol to make essentially propylene, comprising: a) introducing in a reactor a stream comprising the alcohol mixture, optionally water, optionally an inert component, b) contacting said stream with a single catalyst at a temperature above 450° C. in said reactor at conditions effective to dehydrate at least a part of the isobutanol and other alcohols, if any, forming C4⁺ olefins, and to catalytically crack the C4⁺ olefins, wherein the single catalyst is an acid catalyst adapted to cause both the dehydration and the catalytic cracking, c) recovering from said reactor an effluent comprising: ethylene, propylene, water, optionally unconverted alcohols of the alcohol mixture, various hydrocarbons, and the optional inert component of step a), d) fractionating said effluent of step c) to produce at least an ethylene stream, a propylene stream, a fraction consisting essentially of hydrocarbons having 4 carbon atoms or more, water and the optional inert component of step a), optionally recycling ethylene in whole or in part at an inlet of the reactor, optionally recycling the fraction consisting essentially of hydrocarbons having 4 carbon atoms or more at the inlet of the reactor.
 21. The process according to claim 20, wherein, before recycling said hydrocarbons having 4 carbon atoms or more at the inlet of the reactor, said hydrocarbons having 4 carbon atoms or more are sent to a second fractionator to purge the heavies comprising hydrocarbons having more than 4 carbon atoms, water and optionally oxygenates.
 22. The process according to claim 20, wherein the alcohol mixture is subjected to purification to reduce a content of metal ions in the alcohol mixture.
 23. The process of claim 22, wherein the metal ions are selected from Na, Fe, K, Ca and Al.
 24. The process according to claim 20, wherein the temperature in the reactor of step a) and b) is up to 650° C.
 25. The process according to claim 20, further comprising reacting ethylene with 2-butene from the fraction consisting essentially of hydrocarbons having 4 carbon atoms or more recovered at step d) to produce propylene.
 26. The process according to claim 20, further comprising recovering n-butenes from the fraction consisting essentially of hydrocarbons having 4 carbon atoms or more recovered at step d) and reacting the n-butenes in an automethathesis to produce propylene and pentenes.
 27. The process according to claim 20, further comprising fermenting carbohydrates coming from a biomass, or from a syngas route or from a base-catalysed Guerbet condensation to obtain the isobutanol.
 28. The process according to claim 20, further comprising producing the isobutanol by the direct 2-keto acid pathway from carbohydrates that are isolated from biomass.
 29. The process according to claim 20, wherein ethylene is further polymerized optionally with one or more comonomers.
 30. The process according to claim 20, wherein propylene is further polymerized optionally with one or more comonomers.
 31. The process according to claim 20, wherein the single catalyst is a crystalline silicate containing at least one 10 member ring in the structure thereof.
 32. The process according to claim 31, wherein the crystalline silicate is an MFI, MEL, FER, MTT, MWW, TON, EUO, MFS, CON or ZSM-48.
 33. The process according to claim 31, wherein the crystalline silicate is ZSM-5, silicalite-1, boralite C, TS-1, ZSM-11, silicalite-2, boralite D, TS-2, SSZ-46, Ferrierite, FU-9, ZSM-35, ZSM-23, MCM-22, PSH-2, ITQ-1, MCM-49, ZSM-22, Theta-1, NU 10, ZSM-50, EU-1, ZSM-57, CIT-1, or ZSM-48.
 34. The process according to claim 31, wherein the crystalline silicate is a dealuminated crystalline silicate.
 35. The process according to claim 31, wherein the crystalline silicate has a Si/Al ratio of at least
 100. 36. The process of claim 35, wherein the crystalline silicate is an MFI or MEL and is modified with at least 0.1 weight percent of Mg, Ca, La, Ni, Ce, Zn, Co, Ag, Fe or Cu.
 37. The process of claim 31, wherein the crystalline silicate is mixed with a binder.
 38. The process of claim 37, wherein the binder is selected from clays, silica, metal silicate, metal borates, metal oxides, and gels including mixtures of silica and metal oxides. 